A process for hydroliquefaction and / or lightening of a carbonaceous feedstock and an apparatus for carrying it out

Abstract

The present application provides a method for hydroliquefaction and / or lightening of carbon-containing raw material and a device for implementing the method, which can process coal, biomass, industrial and domestic waste and poor / heavy oil to obtain liquid hydrocarbon. The slurry reactor in the device is a suspended bed reactor, which is simple in system, easy to control, does not need an external circulation pump, optimally utilizes the slurry of liquefaction residue on line, is beneficial to obtain reasonable material distribution, realizes self-balance of solvent and improves oil yield. The method adopts cyclone feeding mode, thereby achieving the purpose of reducing coking.

Description

Technical Field

[0001] This invention belongs to the fields of petrochemical and coal chemical industries, and relates to a method for hydrogenating and / or lightening carbon-containing raw materials and an apparatus for implementing the method. Background Technology

[0002] With the increasing demand for liquid fuels and the decreasing available reserves of petroleum resources, liquefaction technology, which converts solid fuels such as coal into liquid fuels, chemical raw materials, and products through chemical processing, has become one of the effective methods to compensate for the shortage of petroleum resources. At the same time, the effective utilization of other carbon-containing resources (such as biomass, industrial and domestic waste, and low-quality / heavy oil) is also gradually attracting attention.

[0003] Coal liquefaction methods are mainly divided into two categories: direct liquefaction and indirect liquefaction. Direct coal liquefaction usually refers to the process of cracking and hydrogenating coal under high temperature and high pressure conditions to change the hydrogen-carbon atomic ratio of the system, thereby liquefying the coal into crude oil, which can then be further processed into refined oil.

[0004] The core of direct coal liquefaction (DCL) technology lies in the cracking, hydrogenation, and product separation of coal. Given the high-polymer macromolecular network structure of coal and its chemical composition containing C, H, N, S, O, and mineral elements, DCL processes often employ stringent conversion conditions (~450℃, ~20MPa H2, catalysis), utilizing free radical reactions to transform coal into liquid fuels or chemicals. The products range from non-condensable gases, gaseous hydrocarbons, liquid hydrocarbons, bituminous substances, and tar to coke, exhibiting a wide variety and distribution. They also contain corrosive substances such as acids and alkalis. Therefore, the success of this technology, especially its efficiency, depends not only on the reaction conditions but also on the process itself and the coupling between different processes.

[0005] CN101220286A provides a coal-oil co-processing technology that mixes pulverized coal with solvent oil (including petroleum residue oil and coal liquefaction heavy oil) to form a coal slurry. The pulverized coal content in the coal slurry is 40%–50%. In two or more upflow slurry-bed reactors, coal is hydrocracking, and the resulting crude oil is hydrorefined into finished oil. This process optimizes the composition of solvent oil in traditional coal-oil co-processing and direct coal liquefaction technologies, increasing the solids content of the coal slurry and reducing secondary cracking of the liquefied oil. However, it requires the simultaneous use of petroleum residue oil and coal liquefaction heavy oil, and the dynamic adjustment of their proportions based on their properties, increasing the complexity of the process.

[0006] CN109554185A discloses a method and system for direct coal liquefaction to produce oil products. This method connects several slurry-bed reactors or suspended-bed reactors with forced circulation in series to achieve multi-stage direct coal liquefaction. By regulating the load of each reactor through external circulation of the circulating slurry or a combination of external and self-circulation, the fluctuation of operating conditions during the reaction process is reduced, while also minimizing coking in the reactors. However, this method is complex, has high equipment investment and operating costs, and involves high hydrogen partial pressures (16-23 MPa), placing stringent requirements on the reaction equipment.

[0007] CN101348726B discloses a direct coal liquefaction method. Coal, solvent, main catalyst, and co-catalyst are mixed uniformly and placed in a reactor. After nitrogen purging, the reactor is filled with methane, and the reaction is carried out for 0.5-4 hours at a total pressure of 7-12 MPa. This technology does not use hydrogen, and the pressure is relatively low compared to existing technologies, reducing the pressure requirements of the equipment. However, the coal conversion rate and oil yield are relatively low. The co-catalyst, fuming sulfuric acid, is a controlled chemical (corrosive, precursor chemical -3), commonly classified as a Class 8.1 acidic corrosive substance, and is highly corrosive to equipment. The co-catalyst sulfur trioxide is a strong oxidizing agent, and when exposed to moisture, it is highly corrosive to most metals.

[0008] Overall, existing direct coal liquefaction technologies mostly employ external circulation series reactors, resulting in complex process control and significant challenges in external circulation pump erosion. While existing internal circulation technologies eliminate the problems associated with external circulation, circulation efficiency is often insufficient, and reactor coking remains a concern. The complex material systems and demanding reaction conditions continue to present challenges and room for improvement in process and equipment design. Summary of the Invention

[0009] To further improve the efficiency, ease of operation, and adaptability to various carbon-containing feedstocks of existing direct coal liquefaction technology, reduce equipment investment, operating costs, and operational difficulty, and simultaneously reduce coking in the reactor, this invention provides a method for hydrogenating and / or lightening carbon-containing feedstocks, as well as an apparatus for implementing this method. The method and apparatus of this invention can process coal, biomass, industrial and domestic waste, and low-quality / heavy oil to obtain liquefied hydrocarbons. The slurry reactor in the apparatus of this invention is a suspended bed reactor, which is simple, easy to control, and requires no external circulation pump. The liquefaction residue slurry is optimized and utilized online, which is beneficial for obtaining a reasonable material distribution, achieving solvent self-balancing, and improving oil yield. The method of this invention reduces coking by preparing the feedstock into a slurry and feeding it directly into the slurry reactor using a cyclone feed method, combined with timely product separation.

[0010] In one aspect, the present invention provides a method for hydrogenating and / or lightening a carbon-containing feedstock, wherein the method comprises:

[0011] (1) After pretreatment of carbon-containing raw materials, they are mixed with solvent oil and catalyst to obtain reaction slurry;

[0012] (2) The reaction slurry is fed into the reactor of the slurry reaction system in a swirling feed manner to react and obtain the light product and the heavy product of the slurry reaction system.

[0013] (3) The light products of the slurry reaction system are subjected to cyclone separation to obtain cyclone-separated light products and cyclone-separated heavy products;

[0014] (4) The light products separated by cyclone separation are subjected to hot high-pressure separation to obtain hot high-pressure oil and hot high-pressure gas;

[0015] (5) The hot high-pressure gas is subjected to cold high-pressure separation to obtain cold high-pressure oil and cold high-pressure separator tail gas;

[0016] (6) The heavy product of the slurry reaction system is separated into gas and liquid in gas-liquid separation system I to obtain light product and heavy product of gas-liquid separation system I.

[0017] (7) Collect the light products of the gas-liquid separation system I into condensate to obtain condensate collection tank oil and condensate collection tank tail gas.

[0018] (8) After combining the hot high-temperature oil, the cold high-temperature oil, and the condensate collection tank oil, the oil is purified to obtain purified crude oil and crude oil purification system exhaust gas.

[0019] (9) After combining the heavy product from the cyclone separation, the heavy product from the gas-liquid separation system I, and the tar obtained in the subsequent step (13), the product is fractionated in the fractionation system I to obtain oil residue slurry, <520℃ distillate oil, and tail gas from the fractionation system I; a portion or all of the <520℃ distillate oil is combined with the purified crude oil to obtain the feed to the oil upgrading reactor, and the remaining portion or all of the <520℃ distillate oil is optionally used as the solvent oil;

[0020] (10) The feed to the oil upgrading reactor is subjected to upgrading treatment to obtain the product of the oil upgrading reactor;

[0021] (11) The product of the oil upgrading reactor is separated into gas and liquid in gas-liquid separation system II to obtain heavy product of gas-liquid separation system II and tail gas of gas-liquid separation system II.

[0022] (12) The heavy product of the gas-liquid separation system II is fractionated in the fractionation system II to obtain wax oil, diesel oil, aviation kerosene, naphtha and tail gas of the fractionation system II; optionally, a portion or all of the wax oil is used as the solvent oil and the remaining portion or all of the wax oil is discharged as the product.

[0023] (13) The oil residue slurry is processed to obtain coke, tar and tail gas of the oil residue slurry treatment system;

[0024] (14) The tail gas from the cold high-pressure separator, the tail gas from the condensate collection tank, the tail gas from the crude oil purification system, the tail gas from fractionation system I, the tail gas from gas-liquid separation system II, and the tail gas from the oil residue slurry treatment system are combined, separated, enriched, and purified to obtain hydrogen, dry gas, liquefied petroleum gas (LPG), and C5. + Hydrocarbons and sulfur; optionally, the hydrogen is combined with fresh hydrogen and recycled.

[0025] In another aspect, the present invention provides an apparatus for carrying out the above-described method, the apparatus comprising a slurry preparation system, a slurry reaction system, a product separation system, an oil upgrading system, an oil residue slurry treatment system, and a tail gas treatment system connected in a fluid communication manner, wherein...

[0026] The slurry reaction system includes a cyclone feeder, a reactor, and one or more cyclone separators. The reactor is a gas-liquid-solid three-phase suspension bed (also known as a "slurry bed") reactor. The reactor includes a reactor shell, a central tube, a gas distributor, a raw material slurry inlet, a light product outlet, and a heavy product outlet. The raw material slurry inlet is connected to the cyclone feeder in fluid communication. The cyclone separator is located inside or outside the reactor.

[0027] The product separation system includes a light product separation system and a heavy product separation system. The light product separation system includes a cyclone separator, a hot high-pressure separator, a cold high-pressure separator, and a crude oil purification system. The heavy product separation system includes a gas-liquid separation system I, a condensate collection tank, and a fractionation system I. The cyclone separator is fluidly connected to the light product outlet of the reactor or the outlet of the cyclone separator, and the gas-liquid separation system I is fluidly connected to the heavy product outlet of the reactor.

[0028] The oil upgrading system includes an oil upgrading reactor, a gas-liquid separation system II, and a fractionation system II.

[0029] The method and apparatus described in this invention can achieve the following beneficial effects: the reactor in the slurry reaction system is a suspended bed reactor, which is simple, easy to control, and does not require an external circulation pump; preparing carbon-containing raw materials into slurry and using a swirling feeding method at the reactor inlet can create a strong spiral flow in the reactor, resulting in a material distribution that is conducive to chemical reaction. Combined with timely separation of products, this achieves the purpose of enhancing heat and mass transfer, gas-liquid-solid mixing, and reducing coking; the light and heavy product outlets of the reactor are connected to suitable separation devices, which can realize online optimized utilization of liquefied residue slurry, which is conducive to obtaining a reasonable material distribution, achieving solvent self-balancing, and improving oil yield.

[0030] In this invention, the inventors discovered that because the material system involved is a heavy carbonaceous substance and the operating temperature is high, it is prone to coking, and the coking phenomenon is more severe when the material is left to stand. To address this problem, the inventors discovered through research that using swirling feeding, which keeps the material in a state of vigorous agitation within the reactor, can reduce coking. Attached Figure Description

[0031] The accompanying drawings are part of the specification and, together with the detailed description, provide a further explanation of the invention, but are not intended to limit the invention.

[0032] Figure 1 This is a schematic diagram of an exemplary process flow for the hydrogenation / liquidation of carbon-containing feedstocks according to the present invention.

[0033] Figures 2a-2e This is a schematic diagram of an exemplary gas-liquid-solid three-phase suspended bed reactor of the present invention, wherein, Figure 2a This illustrates a scenario where only a cyclone separator is installed at the top of the reactor. Figure 2b This illustrates the case where the cyclone separator is installed only outside the reactor; Figures 2c-2e Top views of the reactor are shown.

[0034] Figure 1 The reference numerals in the accompanying drawings are explained as follows: (I) Slurry preparation system; (II) Slurry reaction system; (III) Cyclone separation system; (IV) Hot high-pressure separator; (V) Cold high-pressure separator; (VI) Gas-liquid separation system I; (VII) Condensate collection tank; (VIII) Crude oil purification system; (IX) Fractionation system I; (X) Oil upgrading reactor; (XI) Gas-liquid separation system II; (XII) Fractionation system II; (XIII) Oil residue slurry treatment system; (XIV) Tail gas treatment system.

[0035] Figures 2a-2eThe following are explanations of the reference numerals in the attached figures: (1) Reactor shell (also known as "cylinder"); (2) Central tube; (3) Baffle; (4) Bottom hemispherical end cap; (5) Top hemispherical end cap; (6) Gas phase space; (7) Cyclone separator; (8) Light product outlet; (9) Cylinder outside the reactor; (10) Liquid phase outlet of the cyclone separator; (11) Conical plate; (12) Gas distributor; (13) Gas pre-distribution zone; (14) Gas inlet; (15) Gas pre-distributor; (16) Gas distribution ring pipe; (17) Gas distribution ring pipe located inside the central tube; (18) Gas distribution ring pipe located in the annular area formed by the central tube and the cylinder; (19) Transition pipe; (20) Jet nozzle; (21) Raw material slurry inlet; (22) Cyclone feeder; (23) Heavy product outlet. Detailed Implementation

[0036] The specific embodiments of the present invention will be described in detail below. The specific embodiments described herein are for illustrative and explanatory purposes only and are not intended to limit the scope of the invention.

[0037] In this invention, unless otherwise stated, the term "part" or "a portion" refers to some of the objects modified by the term, for example, it may represent any value in the range of greater than 0% to less than 100% relative to the total amount of the objects modified by the term.

[0038] In one embodiment, the present invention provides a method for hydrogenating and / or lightening a carbon-containing feedstock, wherein the method includes:

[0039] (1) After pretreatment of carbon-containing raw materials, they are mixed with solvent oil and catalyst to obtain reaction slurry;

[0040] (2) The reaction slurry is fed into the reactor of the slurry reaction system in a swirling feed manner to react and obtain the light product and the heavy product of the slurry reaction system.

[0041] (3) The light products of the slurry reaction system are subjected to cyclone separation to obtain cyclone-separated light products and cyclone-separated heavy products;

[0042] (4) The light products separated by cyclone separation are subjected to hot high-pressure separation to obtain hot high-pressure oil and hot high-pressure gas;

[0043] (5) The hot high-pressure gas is subjected to cold high-pressure separation to obtain cold high-pressure oil and cold high-pressure separator tail gas;

[0044] (6) The heavy product of the slurry reaction system is separated into gas and liquid in gas-liquid separation system I to obtain light product and heavy product of gas-liquid separation system I.

[0045] (7) Collect the light products of the gas-liquid separation system I into condensate to obtain condensate collection tank oil and condensate collection tank tail gas.

[0046] (8) After combining the hot high-temperature oil, the cold high-temperature oil, and the condensate collection tank oil, the oil is purified to obtain purified crude oil and crude oil purification system exhaust gas.

[0047] (9) After combining the heavy product from the cyclone separation, the heavy product from the gas-liquid separation system I, and the tar obtained in the subsequent step (13), the product is fractionated in the fractionation system I to obtain oil residue slurry, <520℃ distillate oil, and tail gas from the fractionation system I; a portion or all of the <520℃ distillate oil is combined with the purified crude oil to obtain the feed to the oil upgrading reactor, and the remaining portion or all of the <520℃ distillate oil is optionally used as the solvent oil;

[0048] (10) The feed to the oil upgrading reactor is subjected to upgrading treatment to obtain the product of the oil upgrading reactor;

[0049] (11) The product of the oil upgrading reactor is separated into gas and liquid in gas-liquid separation system II to obtain heavy product of gas-liquid separation system II and tail gas of gas-liquid separation system II.

[0050] (12) The heavy product of the gas-liquid separation system II is fractionated in the fractionation system II to obtain wax oil, diesel oil, aviation kerosene, naphtha and tail gas of the fractionation system II; optionally, a portion or all of the wax oil is used as the solvent oil and the remaining portion or all of the wax oil is discharged as the product.

[0051] (13) The oil residue slurry is processed to obtain coke, tar and tail gas of the oil residue slurry treatment system;

[0052] (14) The tail gas from the cold high-pressure separator, the tail gas from the condensate collection tank, the tail gas from the crude oil purification system, the tail gas from fractionation system I, the tail gas from gas-liquid separation system II, and the tail gas from the oil residue slurry treatment system are combined, separated, enriched, and purified to obtain hydrogen, dry gas, liquefied petroleum gas (LPG), and C5. + Hydrocarbons and sulfur; optionally, the hydrogen is combined with fresh hydrogen and recycled.

[0053] In this invention, the carbon-containing raw material may be selected from, but is not limited to, one or more of the following materials: coal (including coal of different metamorphic degrees, such as lignite and bituminous coal), biomass (such as agricultural waste, plant and biological excrement), industrial and domestic waste (such as waste tires, waste plastics and domestic sludge), low-quality / heavy oil (such as heavy oil in original geological reserves, heavy oil by-products of petroleum refining and processing, heavy oil and asphalt extracted from oil sands and oil shale, and tar and oil residue slurry by-products of the thermal processing of the carbon-containing raw material).

[0054] In some preferred embodiments, the pretreatment of carbon-containing raw materials in step (1) refers to drying and grinding the carbon-containing raw materials into powder or slurry.

[0055] In some preferred embodiments, the catalyst in step (1) is a conventional suspended bed (slurry bed) hydrogenation catalyst known in the art. Preferably, the catalyst comprises one or more selected from natural iron-bearing minerals (e.g., pyrite, pyrrhotite, magnetite, hematite, limonite, siderite) or iron oxides and their salts as the main active component. More preferably, the catalyst is the catalyst described in CN105363450B (e.g., the catalyst prepared in Examples 1-9). For example, the catalyst is selected from any of the following: (i) an iron-based emulsifiable concentrate catalyst composed of FeOOH with kaolin, ZnO, W and Mo, such as an iron-based emulsifiable concentrate catalyst containing 11 wt% kaolin, 7 wt% ZnO, 0.1 wt% W and 0.5 wt% Mo; (ii) an iron-based catalyst composed of Fe2O3 with coke powder, MnO2 and ZnO, such as an iron-based emulsifiable concentrate catalyst containing 18 wt% coke powder, 9 wt% MnO2 and 5 wt% ZnO; (iii) an iron-based powder catalyst composed of Fe2O3 with clay, CaO and Mo, such as an iron-based powder catalyst containing 15 wt% clay, 7 wt% CaO and 0.1 wt% Mo.

[0056] In some preferred embodiments, the solvent oil in step (1) is one or more of the following: inferior oil / heavy oil and its hydrogenated products, coal tar and its hydrogenated products, coal tar distillate oil and its hydrogenated products, <520℃ distillate oil obtained in step (9) and its hydrogenated products, or wax oil obtained in step (12) and its hydrogenated products.

[0057] In some preferred embodiments, in step (1), the carbon-containing raw material, solvent oil and catalyst are mixed in a mass ratio of 100:(0-250):(0.1-5), wherein the amount of the catalyst is based on the active metal therein.

[0058] In some preferred embodiments, the reaction conditions in step (2) are: temperature 400℃-480℃ (e.g. 420℃, 435℃, 455℃, 470℃), hydrogen pressure 2-10MPa (e.g. 5MPa, 6MPa, 8MPa, 9MPa), and average residence time 15-120min (e.g. 30min, 40min, 60min, 80min, 90min, 100min).

[0059] In some preferred embodiments, in step (3), a cyclone separation system is used for cyclone separation. Preferably, the cyclone separation system consists of one or more conventional cyclone separators known in the art.

[0060] In some preferred embodiments, in step (4), the conditions for the hot high-pressure separation are: temperature 200-450℃ (e.g. 220℃, 250℃, 280℃, 300℃, 320℃, 350℃, 400℃) and pressure 2-10MPa (e.g. 3MPa, 5MPa, 6MPa, 8MPa).

[0061] In some preferred embodiments, in step (5), the conditions for cold high-pressure separation are: temperature 0-80℃ (e.g. 5℃, 10℃, 20℃, 25℃, 30℃, 40℃, 45℃, 55℃, 65℃) and pressure 2-10MPa (e.g. 3MPa, 5MPa, 8MPa).

[0062] In some preferred embodiments, in step (6), the gas-liquid separation is performed using a single or series conventional gas-liquid separator known in the art, for example, using a series high-pressure gas-liquid separator + low-pressure gas-liquid separator or a hydrocyclone separator.

[0063] In some preferred embodiments, in step (7), the condensate is collected using a conventional condensate collector known in the art, which may consist of one or more settling tanks.

[0064] In some preferred embodiments, in step (8), the purification process is carried out using one or more of the conventional methods known in the art, such as filtration, centrifugation, sedimentation and fractionation.

[0065] In some preferred embodiments, in step (9), the fractionation is performed using conventional vacuum distillation or a combination of atmospheric and vacuum distillation methods known in the art.

[0066] In some preferred embodiments, in step (10), a conventional oil upgrading reactor (e.g., fixed bed, trickle bed, fluidized bed) known in the art is used for the upgrading process; preferably, the upgrading conditions are: temperature 280-410℃ (e.g., 300℃, 350℃, 360℃, 380℃, 400℃), pressure 5-25MPa, hydrogen / oil volume ratio 800-3000 (e.g., 1000-3000), and volume hourly space velocity 0.2-2h. -1 (e.g., 0.5h) -1 1h -1 1.5h -1 ).

[0067] In some preferred embodiments, in step (11), the gas-liquid separation is performed using a single or series conventional gas-liquid separator known in the art, for example, using a series high-pressure gas-liquid separator + low-pressure gas-liquid separator or a hydrocyclone separator.

[0068] In some preferred embodiments, in step (12), the fractionation is performed using atmospheric distillation or a combination of atmospheric and vacuum distillation, methods known in the art.

[0069] In some preferred embodiments, in step (13), the oil residue slurry is treated using methods such as fluidized bed coking, delayed coking, and / or solvent extraction; preferably, the oil residue slurry is treated using fluidized bed coking or solvent extraction (e.g., NMP solvent extraction). In some preferred embodiments, the temperature of the fluidized bed coking is 500-800°C (e.g., 500-650°C); in other preferred embodiments, the temperature of the delayed coking is 500-700°C, for example, 700°C.

[0070] In some preferred embodiments, in step (14), the separation and enrichment of the exhaust gas are carried out using conventional processes known in the art, such as pressure swing adsorption, membrane separation or cryogenic separation; the purification treatment of the exhaust gas is carried out using conventional processes known in the art, such as amine absorption, liquid phase oxidation-reduction, copper washing, crystallization sulfur method, Claus sulfur recovery method.

[0071] In another embodiment, the present invention provides an apparatus for implementing the above-described method, the apparatus comprising a slurry preparation system, a slurry reaction system, a product separation system, an oil upgrading system, an oil residue slurry treatment system, and a tail gas treatment system connected in fluid communication, wherein...

[0072] The slurry reaction system includes a cyclone feeder, a reactor, and one or more cyclone separators. The reactor is a gas-liquid-solid three-phase suspended bed reactor. The reactor includes a reactor shell, a central tube, a gas distributor, a raw material slurry inlet, a light product outlet, and a heavy product outlet. The raw material slurry inlet is connected to the cyclone feeder in fluid communication. The cyclone separator is located inside or outside the reactor.

[0073] The product separation system includes a light product separation system and a heavy product separation system. The light product separation system includes a cyclone separator, a hot high-pressure separator, a cold high-pressure separator, and a crude oil purification system. The heavy product separation system includes a gas-liquid separation system I, a condensate collection tank, and a fractionation system I. The cyclone separator is fluidly connected to the light product outlet of the reactor or the outlet of the cyclone separator, and the gas-liquid separation system I is fluidly connected to the heavy product outlet of the reactor.

[0074] The oil upgrading system includes an oil upgrading reactor, a gas-liquid separation system II, and a fractionation system II.

[0075] In this document, the slurry reaction system may include one or more reactors, preferably a single reactor.

[0076] In some preferred embodiments, the reactor shell includes a cylindrical body, a bottom hemispherical end cap, and a top hemispherical end cap.

[0077] In some preferred embodiments, the gas distributor is located at the bottom of the reactor, and the gas distributor includes a gas inlet, a gas pre-distributor, a gas pre-distribution zone, a baffle, a transition pipe, and a gas distribution ring pipe.

[0078] Preferably, the partition is disposed between the cylindrical body and the bottom hemispherical end cap. More preferably, a central tube is disposed at the center of the cylindrical body, one end of the central tube is fixed to the partition, and the other end of the central tube is not connected to the top hemispherical end cap.

[0079] In some preferred embodiments, the cyclone separator in the slurry reaction system is located at the top of the reactor (e.g., Figure 2a (as shown), or disposed within a second cylindrical body located outside the reactor and in fluid communication with the reactor (e.g. Figure 2b (As shown). More preferably, a conical plate is installed below the liquid phase outlet of the cyclone separator.

[0080] In some preferred embodiments, the space between the bottom hemispherical end cap of the reactor and the baffle plate is a gas pre-distribution zone, and the gas distribution ring pipe is disposed on the upper plane of the baffle plate; preferably, a portion of the gas distribution ring pipe is located inside the central pipe, and the remaining portion is located within the annular area formed by the central pipe and the cylindrical body. More preferably, the transition pipe is vertically inserted into and fixed on the baffle plate, and is in fluid communication with the gas pre-distribution zone and the gas distribution ring pipe. Even more preferably, a side-down jet hole is formed on the gas distribution ring pipe.

[0081] In some preferred embodiments, the partition and each component it contacts are in close fit.

[0082] In some preferred embodiments, the gas pre-distributor is located at the bottom of the reactor and is used to pre-distribute the gas.

[0083] In some preferred embodiments, the raw material slurry inlet is located at the lower part of the cylindrical body of the reactor; more preferably, the slurry feed pipe connected to the raw material slurry inlet forms an angle of 10-60 degrees with the wall of the reactor.

[0084] In some preferred embodiments, the heavy product outlet is located at the bottom of the reactor. Preferably, one end of the discharge pipe connected to the heavy product outlet is connected to the central pipe. More preferably, the discharge pipe passes through the baffle and the bottom hemispherical end cap of the reactor.

[0085] In some preferred embodiments, the light product outlet is located at the top of the reactor.

[0086] Exemplary embodiments of the present invention can be illustrated by the following numbered paragraphs:

[0087] 1. A method for hydrogenating and / or lightening a carbon-containing feedstock, wherein the method comprises:

[0088] (1) After pretreatment of carbon-containing raw materials, they are mixed with solvent oil and catalyst to obtain reaction slurry;

[0089] (2) The reaction slurry is fed into the reactor of the slurry reaction system in a swirling feed manner to react and obtain the light product and the heavy product of the slurry reaction system.

[0090] (3) The light products of the slurry reaction system are subjected to cyclone separation to obtain cyclone-separated light products and cyclone-separated heavy products;

[0091] (4) The light products separated by cyclone separation are subjected to hot high-pressure separation to obtain hot high-pressure oil and hot high-pressure gas;

[0092] (5) The hot high-pressure gas is subjected to cold high-pressure separation to obtain cold high-pressure oil and cold high-pressure separator tail gas;

[0093] (6) The heavy product of the slurry reaction system is separated into gas and liquid in gas-liquid separation system I to obtain light product and heavy product of gas-liquid separation system I.

[0094] (7) Collect the light products of the gas-liquid separation system I into condensate to obtain condensate collection tank oil and condensate collection tank tail gas.

[0095] (8) After combining the hot high-temperature oil, the cold high-temperature oil, and the condensate collection tank oil, the oil is purified to obtain purified crude oil and crude oil purification system exhaust gas.

[0096] (9) After combining the heavy product from the cyclone separation, the heavy product from the gas-liquid separation system I, and the tar obtained in the subsequent step (13), the product is fractionated in the fractionation system I to obtain oil residue slurry, <520℃ distillate oil, and tail gas from the fractionation system I; a portion or all of the <520℃ distillate oil is combined with the purified crude oil to obtain the feed to the oil upgrading reactor, and the remaining portion or all of the <520℃ distillate oil is optionally used as the solvent oil;

[0097] (10) The feed to the oil upgrading reactor is subjected to upgrading treatment to obtain the product of the oil upgrading reactor;

[0098] (11) The product of the oil upgrading reactor is separated into gas and liquid in gas-liquid separation system II to obtain heavy product of gas-liquid separation system II and tail gas of gas-liquid separation system II.

[0099] (12) The heavy product of the gas-liquid separation system II is fractionated in the fractionation system II to obtain wax oil, diesel oil, aviation kerosene, naphtha and tail gas of the fractionation system II; optionally, a portion or all of the wax oil is used as the solvent oil and the remaining portion or all of the wax oil is discharged as the product.

[0100] (13) The oil residue slurry is processed to obtain coke, tar and tail gas of the oil residue slurry treatment system;

[0101] (14) The tail gas from the cold high-pressure separator, the tail gas from the condensate collection tank, the tail gas from the crude oil purification system, the tail gas from fractionation system I, the tail gas from gas-liquid separation system II, and the tail gas from the oil residue slurry treatment system are combined, separated, enriched, and purified to obtain hydrogen, dry gas, liquefied petroleum gas (LPG), and C5. + Hydrocarbons and sulfur; optionally, the hydrogen is combined with fresh hydrogen and recycled.

[0102] 2. The method as described in paragraph 1, wherein the carbon-containing raw material is one or more selected from the following materials: coal, biomass, industrial and domestic waste, and low-quality / heavy oil.

[0103] 3. The method as described in paragraph 1 or 2, wherein in step (1), the pretreatment is to dry and grind the carbon-containing raw material into powder or slurry.

[0104] 4. The method described in any of paragraphs 1-3, wherein the catalyst described in step (1) is a suspended bed hydrogenation catalyst.

[0105] 5. The method described in any of paragraphs 1-4, wherein the solvent oil in step (1) is one or more of the following: inferior oil / heavy oil and its hydrogenated products, coal tar and its hydrogenated products, coal tar distillate oil and its hydrogenated products, <520℃ distillate oil obtained in step (9) and its hydrogenated products, or wax oil obtained in step (12) and its hydrogenated products.

[0106] 6. The method as described in any of paragraphs 1-5, wherein in step (1), the carbon-containing raw material, solvent oil and catalyst are mixed in a mass ratio of 100:(0-250):(0.1-5), and the amount of the catalyst is based on the active metal therein.

[0107] 7. The method described in any of paragraphs 1-6, wherein in step (2), the reaction conditions are: temperature 400℃-480℃, hydrogen pressure 2-10MPa, and average residence time 15-120min.

[0108] 8. The method described in any of paragraphs 1-7, wherein, in step (3), a cyclone separation system is used to perform the cyclone separation.

[0109] 9. The method described in any of paragraphs 1-8, wherein in step (4), the conditions for the thermal high-pressure separation are: temperature 200-450℃ and pressure 2-10MPa.

[0110] 10. The method described in any of paragraphs 1-9, wherein in step (5), the conditions for the cold high-pressure separation are: temperature 0-80℃ and pressure 2-10MPa.

[0111] 11. The method described in any of paragraphs 1-10, wherein in step (6), the gas-liquid separation is performed by using a series of high-pressure gas-liquid separators + low-pressure gas-liquid separators or hydrocyclones.

[0112] 12. The method as described in any of paragraphs 1-11, wherein in step (8), the purification process is performed using one or more methods selected from filtration, centrifugation, sedimentation and fractionation.

[0113] 13. The method described in any of paragraphs 1-12, wherein, in step (9), the fractionation is performed by vacuum distillation or a combination of atmospheric distillation and vacuum distillation.

[0114] 14. The method as described in any of paragraphs 1-13, wherein, in step (10), the upgrading process is carried out using an upgrading reactor.

[0115] 15. The method as described in paragraph 14, wherein the conditions for the upgrading treatment are: temperature 280-410℃, pressure 5-25MPa, hydrogen / oil volume ratio 800-3000, and volume hourly space velocity 0.2-2h. -1 .

[0116] 16. The method described in any of paragraphs 1-15, wherein in step (11), the gas-liquid separation is performed using a series of high-pressure gas-liquid separators + low-pressure gas-liquid separators or hydrocyclones.

[0117] 17. The method described in any of paragraphs 1-16, wherein, in step (12), the fractionation is performed by atmospheric distillation or a combination of atmospheric distillation and vacuum distillation.

[0118] 18. The method as described in any of paragraphs 1-17, wherein, in step (13), the oil residue slurry is treated by fluidized coking, delayed coking and / or solvent extraction.

[0119] 19. The method as described in paragraph 18, wherein the temperature of the fluidized coking is 500-800°C.

[0120] 20. The method as described in paragraph 18, wherein the temperature of the delayed coking is 500-700°C.

[0121] 21. The method described in any of paragraphs 1-20, wherein in step (14), pressure swing adsorption, membrane separation or cryogenic separation is used for the separation and enrichment; and the purification treatment is carried out by alkanolamine absorption, liquid phase oxidation-reduction, copper washing, crystallization sulfur or Claus sulfur recovery.

[0122] 22. An apparatus for carrying out the method described in any one of paragraphs 1-21, the apparatus comprising a slurry preparation system, a slurry reaction system, a product separation system, an oil upgrading system, an oil residue slurry treatment system, and a tail gas treatment system connected in fluid communication, wherein,

[0123] The slurry reaction system includes a cyclone feeder, a reactor, and one or more cyclone separators. The reactor is a gas-liquid-solid three-phase suspended bed reactor. The reactor includes a reactor shell, a central tube, a gas distributor, a raw material slurry inlet, a light product outlet, and a heavy product outlet. The raw material slurry inlet is connected to the cyclone feeder in fluid communication. The cyclone separator is located inside or outside the reactor.

[0124] The product separation system includes a light product separation system and a heavy product separation system. The light product separation system includes a cyclone separator, a hot high-pressure separator, a cold high-pressure separator, and a crude oil purification system. The heavy product separation system includes a gas-liquid separation system I, a condensate collection tank, and a fractionation system I. The cyclone separator is fluidly connected to the light product outlet of the reactor or the outlet of the cyclone separator, and the gas-liquid separation system I is fluidly connected to the heavy product outlet of the reactor.

[0125] The oil upgrading system includes an oil upgrading reactor, a gas-liquid separation system II, and a fractionation system II.

[0126] 23. The apparatus as described in paragraph 22, wherein the reactor shell comprises a cylindrical body, a bottom hemispherical end cap, and a top hemispherical end cap.

[0127] 24. The apparatus as described in paragraph 22 or 23, wherein the gas distributor is disposed at the bottom end of the reactor, the gas distributor comprising a gas inlet, a gas pre-distributor, a gas pre-distribution zone, a baffle, a transition pipe, and a gas distribution ring pipe.

[0128] 25. The apparatus as described in paragraph 24, wherein the partition is disposed between the cylindrical body and the bottom hemispherical end cap.

[0129] 26. The apparatus as described in paragraph 25, wherein a central tube is provided at the center of the cylindrical body, one end of the central tube is fixed to the partition plate, and the other end of the central tube is not connected to the top hemispherical end cap.

[0130] 27. The apparatus as described in any of paragraphs 22-26, wherein the cyclone separator in the slurry reaction system is disposed at the top of the reactor or disposed in a second cylindrical body located outside the reactor and in fluid communication with the reactor.

[0131] 28. The apparatus as described in paragraph 27, wherein a conical plate is installed below the liquid phase outlet of the cyclone separator.

[0132] 29. The apparatus as described in any of paragraphs 24-28, wherein the space between the bottom hemispherical end cap of the reactor and the partition is a gas pre-distribution zone, and the gas distribution ring pipe is disposed on the upper plane of the partition.

[0133] 30. The apparatus as described in paragraph 29, wherein a portion of the air distribution ring tube is located inside the central tube, and the remaining portion of the air distribution ring tube is located within the annular region formed by the central tube and the cylindrical body.

[0134] 31. The apparatus as described in paragraph 29, wherein the transition tube is vertically inserted into and fixed to the partition plate, and is in fluid communication with the gas pre-distribution zone and the gas distribution ring tube.

[0135] 32. The apparatus as described in paragraph 29, wherein a side-down jet port is provided on the air distribution ring pipe.

[0136] 33. The device as described in any of paragraphs 24-32, wherein the partition and each component in contact with it are in close fit.

[0137] 34. The apparatus as described in any of paragraphs 24-33, wherein the gas pre-distributor is located at the bottom end of the reactor.

[0138] 35. The apparatus as described in any of paragraphs 22-34, wherein the feed slurry inlet is located at the lower part of the cylindrical body of the reactor.

[0139] 36. The apparatus as described in any of paragraphs 22-35, wherein the slurry feed pipe connected to the raw material slurry inlet forms an angle of 10-60 degrees with the wall of the reactor.

[0140] 37. The apparatus as described in any of paragraphs 22-36, wherein the heavy product outlet is located at the bottom of the reactor.

[0141] 38. The apparatus as described in paragraph 37, wherein one end of the discharge pipe connected to the heavy product outlet is connected to the central pipe.

[0142] 39. The apparatus as described in paragraph 38, wherein the discharge pipe passes through the partition and the bottom hemispherical end cap of the reactor.

[0143] 40. The apparatus as described in any of paragraphs 22-39, wherein the light product outlet is located at the top of the reactor.

[0144] Next, we will combine Figure 1 An exemplary process flow of the present invention is described below:

[0145] Carbonaceous raw materials selected from coal, biomass, industrial waste, domestic waste, low-quality oil, or heavy oil are pretreated in a slurry preparation system (I) and then mixed with solvent oil and catalyst at a mass ratio of 100:(0-250):(0.1-5) to form a slurry (catalyst is based on active metal). The resulting slurry is fed into a slurry reaction system (II) and reacted under conditions of 400-480℃, 2-10MPa, and an average residence time of 15-120min to obtain light and heavy products of the slurry reaction system.

[0146] The light products from the slurry reaction system are fed into a cyclone separator (III) and separated using conventional methods known in the art to obtain cyclone-separated light and heavy products. The cyclone-separated light products are then fed into a hot high-pressure separator (IV) and separated at a temperature of 200-450°C and a pressure of 2-10 MPa to obtain hot high-pressure oil and hot high-pressure gas. The hot high-pressure gas is then fed into a cold high-pressure separator (V) and separated at a temperature of 0-80°C and a pressure of 2-10 MPa to obtain cold high-pressure oil and cold high-pressure separator tail gas.

[0147] The heavy product from the slurry reaction system is fed into gas-liquid separation system I (VI), where conventional gas-liquid separation equipment (either individually or in series) known in the art is used to obtain the light product from gas-liquid separation system I and the heavy product from gas-liquid separation system I. The light product from gas-liquid separation system I is then sent to condensate collection tank (VII) and collected using conventional methods known in the art to obtain condensate collection tank oil and condensate collection tank tail gas.

[0148] Hot high-density oil, cold high-density oil, and condensate collection tank oil are sent to the crude oil purification system (VIII), where they are treated once or multiple times using one or more of the conventional methods known in the art, such as filtration, centrifugation, sedimentation, and fractionation, to obtain purified crude oil and crude oil purification system exhaust gas.

[0149] The heavy products from the cyclone separation, the heavy products from the gas-liquid separation system I, and the tar are fed into the fractionation system I (IX), where fractionation is carried out using vacuum distillation or a combination of atmospheric and vacuum distillation, as known in the art, to obtain oil residue slurry, <520℃ distillate oil, and tail gas from the fractionation system I; optionally, 0%-100% of the <520℃ distillate oil is fed into the slurry preparation system (I) as a solvent.

[0150] The purified crude oil is combined with the remaining <520℃ fraction and fed into the oil upgrading reactor (X), where it is heated at 280-410℃, 5-25MPa, a hydrogen / oil volume ratio of 800-3000, and a volume hourly space velocity of 0.2-2h. -1 Under certain conditions, oil products are upgraded to obtain the product from the oil upgrading reactor.

[0151] The product from the oil upgrading reactor is fed into the gas-liquid separation system II (XI), where gas-liquid separation is performed using conventional gas-liquid separation methods known in the art, either individually or in series, to obtain the heavy product from the gas-liquid separation system II and the tail gas from the gas-liquid separation system II.

[0152] The heavy product of the gas-liquid separation system II is fed into the fractionation system II (XII) and fractionated using conventional atmospheric distillation or a combination of atmospheric and vacuum distillation methods known in the art to obtain wax oil, diesel oil, aviation kerosene, naphtha and tail gas of the fractionation system II; optionally, 0%-100% of the wax oil is fed into the slurry preparation system (I) for use as solvent oil.

[0153] The oil residue slurry is fed into the slurry treatment system (XIII), and methods such as fluidized coking, delayed coking and / or solvent extraction are used to obtain coke, tar and tail gas of the oil residue slurry treatment system; preferably, the oil residue slurry is treated by fluidized coking or solvent extraction; more preferably, the temperature of fluidized coking is 500-800℃.

[0154] All equipment exhaust gases (including exhaust gases from the cold high-pressure separator, condensate collection tank, crude oil purification system, fractionation system I, gas-liquid separation system II, and oil sludge treatment system) are fed into the exhaust gas treatment system (XIV), where conventional methods known in the art are used for separation, enrichment, and purification to obtain hydrogen, dry gas, liquefied petroleum gas (LPG), and C5. + Hydrocarbons and sulfur. The recovered hydrogen is combined with fresh hydrogen and recycled.

[0155] The exemplary gas-liquid-solid three-phase suspended bed reactor of the present invention is described below with reference to Figure 2:

[0156] like Figure 2a and Figure 2b As shown, the reactor shell includes a cylindrical body (1), a bottom hemispherical head (4), and a top hemispherical head (5). A central tube (2) is installed inside the reactor. One end of the central tube (2) is mounted on a partition (3) between the bottom end of the cylindrical body (1) and the bottom hemispherical head (4). The other end of the central tube is not connected to the top end of the cylindrical body (1) and is at a certain distance from it, forming a gas phase space (6) with the top hemispherical head (5). A light product outlet (8) is located at the top of the reactor. Optionally, a cyclone separator (7) is located in the gas phase space (6) at the top of the reactor. Figure 2a ) or located inside a cylindrical shell (9) outside the reactor. Figure 2b When the optional cyclone separator is set outside the reactor, a conical plate (11) is installed below the liquid phase outlet (10) of the cyclone separator (at different intervals as needed).

[0157] like Figures 2a-2d As shown, the gas distributor (12) is located at the bottom of the reactor and includes a gas inlet (14), a gas pre-distributor (15), a gas pre-distribution zone (13), a baffle (3), a transition pipe (19), and a gas distribution ring pipe (16). The gas distribution ring pipe (16) consists of a gas distribution ring pipe (17) located inside the central pipe and a gas distribution ring pipe (18) located in the annular area formed by the central pipe and the cylinder. The transition pipe (19) passes through the baffle (3) and connects the gas distribution ring pipe (16) and the gas pre-distribution zone (13). A side-mounted jet hole (20) is opened on the gas distribution ring pipe (16). The baffle (3) and the components in contact with it are all tightly fitted.

[0158] like Figure 2a , Figure 2b and Figure 2e The raw material slurry inlet (21) is located at the bottom of the reactor body, and the slurry feed pipe of the cyclone feeder (22) forms an angle of 10-60 degrees with the reactor wall. The heavy product outlet (23) is located at the bottom of the reactor, and one end of the discharge pipe connected to the heavy product outlet is connected to the central pipe (2), passing through the partition (3) and the bottom hemispherical head (4).

[0159] The invention is further illustrated by the following examples, but the invention is not limited thereto.

[0160] Example

[0161] Unless otherwise stated, the reagents, materials and apparatus involved in the following examples are all commercially available in the art; the routine operations involved in the following examples can be found in patents, patent applications and publications disclosed in the art (e.g., He Yongde, ed., Modern Coal Chemical Technology Handbook, Chemical Industry Press, 2003, but not limited thereto).

[0162] Example 1

[0163] The slurry 1 shown in Table 1 was fed into the slurry reaction system by cyclone feeding, and the reaction was carried out under the conditions of temperature 435℃, pressure 5MPa and average residence time 60min to obtain the light product and the heavy product of the slurry reaction system.

[0164] The light products from the slurry reaction system are fed into a cyclone separation system (consisting of two cyclone separators) to obtain cyclone-separated light and heavy products. The cyclone-separated light products are then sent to a hot high-pressure separator for separation at 410℃ and 3MPa to obtain hot high-pressure oil and hot high-pressure gas. The hot high-pressure gas is then sent to a cold high-pressure separator for separation at 40℃ and 2MPa to obtain cold high-pressure oil and cold high-pressure separator tail gas. The heavy products from the slurry reaction system are sent to gas-liquid separation system I (one gravity settling tank) to obtain gas-liquid separation system I light and heavy products. The gas-liquid separation system I light products are then sent to a condensate collection tank (one condensate settling tank) to obtain condensate collection tank oil and condensate collection tank tail gas. The hot high-pressure oil, cold high-pressure oil, and condensate collection tank oil are then sent to a crude oil purification system for purification using gravity settling to obtain purified crude oil and crude oil purification system tail gas. The heavy products from gas-liquid separation system I, the heavy products from cyclone separation, and tar are combined and sent to fractionation system I. Fractionation is carried out by vacuum distillation (top pressure 5 kPaA, top temperature 65°C) to obtain oil residue slurry, <520°C distillate oil, and tail gas from fractionation system I. 100% of the <520°C distillate oil is sent to the slurry preparation system for use as solvent oil.

[0165] The purified crude oil is fed into an oil upgrading reactor (fixed-bed reactor) at a temperature of 360℃, a pressure of 12MPa, a hydrogen / oil volume ratio of 2000, and a volume hourly space velocity of 0.5h⁻¹. -1 Oil upgrading is carried out under specific conditions to obtain the product of the oil upgrading reactor. The product of the oil upgrading reactor is sent to gas-liquid separation system II (one hydrocyclone) to obtain the heavy product of gas-liquid separation system II and the tail gas of gas-liquid separation system II. The heavy product of gas-liquid separation system II is sent to fractionation system II, and fractionation is carried out by a combination of atmospheric distillation (top pressure 148 kPaG, top temperature 150°C) and vacuum distillation (top pressure 5 kPaA, top temperature 65°C) to obtain wax oil, diesel oil, aviation kerosene, naphtha and the tail gas of fractionation system II; 100% of the obtained wax oil is sent to the slurry preparation system for use as solvent oil. The oil residue slurry is sent to the oil residue slurry treatment system and subjected to fluidized coking to obtain coke, tar and the tail gas of the oil residue slurry treatment system. The temperature of the fluidized coking is 500°C.

[0166] The yields of the main products are shown in Table 2.

[0167] Example 2

[0168] The slurry 2 shown in Table 1 is fed into the slurry reaction system by cyclone feeding. The reaction takes place under the conditions of temperature 400℃, pressure 10MPa and average residence time 30min, to obtain light products and heavy products of the slurry reaction system.

[0169] The light products from the slurry reaction system are fed into a cyclone separation system (consisting of two cyclone separators) to obtain cyclone-separated light and heavy products. The cyclone-separated light products are then sent to a hot high-pressure separator for separation at 200°C and 10MPa to obtain hot high-pressure oil and hot high-pressure gas. The hot high-pressure gas is then sent to a cold high-pressure separator for separation at 30°C and 10MPa to obtain cold high-pressure oil and cold high-pressure separator tail gas. The heavy products from the slurry reaction system are fed into gas-liquid separation system I (one gravity settling tank) to obtain gas-liquid separation system I light and heavy products. The gas-liquid separation system I light products are then sent to a condensate collection tank (consisting of two condensate settling tanks) to obtain condensate collection tank oil and condensate collection tank tail gas. Hot high-density oil, cold high-density oil, and condensate collection tank oil are sent to the crude oil purification system for purification using sedimentation and filtration to obtain purified crude oil and crude oil purification system tail gas. The heavy products from gas-liquid separation system I, cyclone separation heavy products, and tar are combined and sent to fractionation system I. Fractionation is performed using a combination of atmospheric distillation (top pressure 148 kPaG, top temperature 150°C) and vacuum distillation (top pressure 5 kPaA, top temperature 65°C) to obtain oil residue slurry, <520°C distillate oil, and fractionation system I tail gas. 30% (v / v) of the <520°C distillate oil is sent to the slurry preparation system for use as solvent oil.

[0170] The purified crude oil and the remaining <520℃ fraction were combined and fed into an oil upgrading reactor (fixed-bed reactor) at a temperature of 410℃, a pressure of 25MPa, a hydrogen / oil volume ratio of 2500, and a volume hourly space velocity of 2h⁻¹. -1 Oil upgrading is carried out under specific conditions to obtain the product of the oil upgrading reactor. The product of the oil upgrading reactor is sent to gas-liquid separation system II (one gravity setter) to obtain the heavy product of gas-liquid separation system II and the tail gas of gas-liquid separation system II. The heavy product of gas-liquid separation system II is sent to fractionation system II and fractionated by atmospheric distillation (top pressure 148 kPaG, top temperature 150℃) to obtain wax oil, diesel oil, aviation kerosene, naphtha and the tail gas of fractionation system II; 100% of the obtained wax oil is sent to the slurry preparation system for use as solvent oil. The oil residue slurry is sent to the oil residue slurry treatment system and fluidized coking is used to obtain coke, tar and the tail gas of the oil residue slurry treatment system. The coking temperature is 800℃.

[0171] The yields of the main products are shown in Table 2.

[0172] Example 3

[0173] The slurry 3 shown in Table 1 is fed into the slurry reaction system by cyclone feeding, and the reaction occurs under the conditions of temperature 455℃, pressure 8MPa and average residence time 120min, to obtain the light product and the heavy product of the slurry reaction system.

[0174] The light products from the slurry reaction system are fed into a cyclone separation system (consisting of two cyclone separators) to obtain cyclone-separated light and heavy products. The cyclone-separated light products are then sent to a hot high-pressure separator for separation at 400℃ and 6MPa to obtain hot high-pressure oil and hot high-pressure gas. The hot high-pressure gas is then sent to a cold high-pressure separator for separation at 80℃ and 3MPa to obtain cold high-pressure oil and cold high-pressure separator tail gas. The heavy products from the slurry reaction system are sent to gas-liquid separation system I (one gravity settling tank) for gas-liquid separation to obtain gas-liquid separation system I light and heavy products. The gas-liquid separation system I light products are then sent to a condensate collection tank (one condensate settling tank) to obtain condensate collection tank oil and condensate collection tank tail gas. Hot high-density oil, cold high-density oil, and condensate collection tank oil are sent to the crude oil purification system for purification using fractional distillation (top pressure 148 kPaG, top temperature 150°C), yielding purified crude oil and tail gas from the crude oil purification system. Heavy products from gas-liquid separation system I, heavy products from cyclone separation, and tar are combined and sent to fractional distillation system I, where they are fractionated using vacuum distillation (top pressure 5 kPaA, top temperature 65°C), yielding oil slurry, <520°C distillate oil, and tail gas from fractional distillation system I.

[0175] The purified crude oil and the <520℃ distillate oil were combined and fed into an oil upgrading reactor (fixed-bed reactor) at a temperature of 280℃, a pressure of 25MPa, a hydrogen / oil volume ratio of 3000, and a volume hourly space velocity of 0.2h⁻¹. -1 Oil upgrading is carried out under specific conditions to obtain the product of the oil upgrading reactor. The product of the oil upgrading reactor is sent to gas-liquid separation system II (one gravity setter) to obtain the heavy product of gas-liquid separation system II and the tail gas of gas-liquid separation system II. The heavy product of gas-liquid separation system II is sent to fractionation system II and fractionated by atmospheric distillation (top pressure 148 kPaG, top temperature 150°C) to obtain wax oil, diesel oil, aviation kerosene, naphtha and the tail gas of fractionation system II; the oil residue slurry is sent to the oil residue slurry treatment system and extracted by NMP solvent to obtain coke, tar and the tail gas of the oil residue slurry treatment system.

[0176] The yields of the main products are shown in Table 2.

[0177] Example 4

[0178] The slurry 4 shown in Table 1 is fed into the slurry reaction system by cyclone feeding. The reaction takes place under the conditions of temperature 430℃, pressure 2MPa, and average residence time 60min, to obtain the light product and the heavy product of the slurry reaction system.

[0179] The light products from the slurry reaction system are fed into a cyclone separation system (consisting of three cyclone separators) to obtain cyclone-separated light and heavy products. The cyclone-separated light products are then sent to a hot high-pressure separator for separation at 320℃ and 2MPa to obtain hot high-pressure oil and hot high-pressure gas. The hot high-pressure gas is then sent to a cold high-pressure separator for separation at 0℃ and 2MPa to obtain cold high-pressure oil and cold high-pressure separator tail gas. The heavy products from the slurry reaction system are sent to gas-liquid separation system I (one gravity settling tank) to obtain gas-liquid separation system I light and heavy products. The gas-liquid separation system I light products are then sent to a condensate collection tank (consisting of two condensate settling tanks) to obtain condensate collection tank oil and condensate collection tank tail gas. The hot high-pressure oil, cold high-pressure oil, and condensate collection tank oil are then sent to a crude oil purification system for purification by filtration to obtain purified crude oil and crude oil purification system tail gas. The heavy products from gas-liquid separation system I, cyclone separation heavy products, and tar are combined and sent to fractionation system I. Fractionation is carried out by vacuum distillation (top pressure 5 kPaA, top temperature 65°C) to obtain oil residue slurry, <520°C distillate oil, and tail gas from fractionation system I. 49% (V / V) of the <520°C distillate oil is sent to the slurry preparation system for use as a solvent.

[0180] The purified crude oil was combined with the remaining <520℃ fraction and fed into an oil upgrading reactor (fixed-bed reactor) at 350℃, 5MPa, a hydrogen / oil volume ratio of 800, and a volume hourly space velocity of 2h⁻¹. -1 Oil upgrading is carried out under specific conditions to obtain the product of the oil upgrading reactor. The product of the oil upgrading reactor is sent to gas-liquid separation system II (one gravity setter) to obtain the heavy product of gas-liquid separation system II and the tail gas of gas-liquid separation system II. The heavy product of gas-liquid separation system II is sent to fractionation system II and fractionated by atmospheric distillation (top pressure 148 kPaG, top temperature 150℃) to obtain wax oil, diesel oil, aviation kerosene, naphtha and the tail gas of fractionation system II; 100% of the obtained wax oil is sent to the slurry preparation system for use as solvent oil. The oil residue slurry is sent to the oil residue slurry treatment system and subjected to delayed coking to obtain coke, tar and the tail gas of the oil residue slurry treatment system. The coking temperature is 700℃.

[0181] The yields of the main products are shown in Table 2.

[0182] Example 5

[0183] The slurry 5 shown in Table 1 is fed into the slurry reaction system by cyclone feeding, and the reaction occurs under the conditions of temperature 480℃, pressure 10MPa and average residence time 15min, to obtain the light product and the heavy product of the slurry reaction system.

[0184] The light products from the slurry reaction system are fed into a cyclone separation system (consisting of three cyclone separators) to obtain cyclone-separated light and heavy products. The cyclone-separated light products are then sent to a hot high-pressure separator for separation at 450°C and 8 MPa to obtain hot high-pressure oil and hot high-pressure gas. The hot high-pressure gas is then sent to a cold high-pressure separator for separation at 55°C and 5 MPa to obtain cold high-pressure oil and cold high-pressure separator tail gas. The heavy products from the slurry reaction system are fed into gas-liquid separation system I (one gravity settling tank) to obtain gas-liquid separation system I light and heavy products. The gas-liquid separation system I light products are then sent to a condensate collection tank (one condensate settling tank) to obtain condensate collection tank oil and condensate collection tank tail gas. Hot high-density oil, cold high-density oil, and condensate collection tank oil are sent to the crude oil purification system for purification using fractional distillation (top pressure 148 kPaG, top temperature 150°C), yielding purified crude oil and tail gas from the crude oil purification system. Heavy products from gas-liquid separation system I, cyclone separation heavy products, and tar are combined and sent to fractionation system I. Fractionation is performed using a combination of atmospheric distillation (top pressure 148 kPaG, top temperature 150°C) and vacuum distillation (top pressure 5 kPaA, top temperature 65°C), yielding oil slurry, <520°C distillate oil, and tail gas from fractionation system I. 60% (v / v) of the <520°C distillate oil is sent to the slurry preparation system for use as a solvent.

[0185] The purified crude oil and the remaining <520℃ fraction were combined and fed into an oil upgrading reactor (fluidized bed reactor) at a temperature of 380℃, a pressure of 25MPa, a hydrogen / oil volume ratio of 1000, and a volume hourly space velocity of 0.5h⁻¹. -1 Oil upgrading is carried out under specific conditions to obtain the product of the oil upgrading reactor. The product of the oil upgrading reactor is sent to gas-liquid separation system II (one gravity setter) to obtain the heavy product of gas-liquid separation system II and the tail gas of gas-liquid separation system II. The heavy product of gas-liquid separation system II is sent to fractionation system II and fractionated by atmospheric distillation (top pressure 148 kPaG, top temperature 150℃) to obtain wax oil, diesel oil, aviation kerosene, naphtha and the tail gas of fractionation system II; 30% (v / v) of the obtained wax oil is sent to the slurry preparation system as solvent oil; the oil residue slurry is sent to the oil residue slurry treatment system and fluidized coking is used to obtain coke, tar and the tail gas of the oil residue slurry treatment system, with a coking temperature of 650℃.

[0186] The yields of the main products are shown in Table 2.

[0187] Comparative Example 1

[0188] The slurry 1 shown in Table 1 was pumped into the slurry reaction system through the feed pipe inserted horizontally at the bottom of the reactor. The reaction took place under the conditions of temperature 435℃, pressure 5MPa, and average residence time 60min, resulting in light and heavy products of the slurry reaction system.

[0189] The light products from the slurry reaction system are fed into a cyclone separation system (consisting of two cyclone separators) to obtain cyclone-separated light and heavy products. The cyclone-separated light products are then sent to a hot high-pressure separator for separation at 410℃ and 3MPa to obtain hot high-pressure oil and hot high-pressure gas. The hot high-pressure gas is then sent to a cold high-pressure separator for separation at 40℃ and 2MPa to obtain cold high-pressure oil and cold high-pressure separator tail gas. The heavy products from the slurry reaction system are sent to gas-liquid separation system I (one gravity settling tank) to obtain gas-liquid separation system I light and heavy products. The gas-liquid separation system I light products are then sent to a condensate collection tank (one condensate collection tank) to obtain condensate collection tank oil and condensate collection tank tail gas. The hot high-pressure oil, cold high-pressure oil, and condensate collection tank oil are then sent to a crude oil purification system for purification using gravity settling to obtain purified crude oil and crude oil purification system tail gas. The heavy products from gas-liquid separation system I, cyclone separation heavy products, and tar are combined and sent to fractionation system I. Fractionation is carried out by vacuum distillation (top pressure 5 kPaA, top temperature 65°C) to obtain oil residue slurry, <520°C distillate oil, and tail gas from fractionation system I. 100% of the <520°C distillate oil is sent to the slurry preparation system for use as a solvent.

[0190] The purified crude oil is fed into an oil upgrading reactor (fixed-bed reactor) at a temperature of 360℃, a pressure of 12MPa, a hydrogen / oil volume ratio of 2000, and a volume hourly space velocity of 0.5h⁻¹. -1 Oil upgrading is carried out under specific conditions to obtain the product of the oil upgrading reactor. The product of the oil upgrading reactor is sent to gas-liquid separation system II (one gravity setter) to obtain the heavy product of gas-liquid separation system II and the tail gas of gas-liquid separation system II. The heavy product of gas-liquid separation system II is sent to fractionation system II, and fractionation is carried out by a combination of atmospheric distillation (top pressure 148 kPaG, top temperature 150℃) and vacuum distillation (top pressure 5 kPaA, top temperature 65℃) to obtain wax oil, diesel oil, aviation kerosene, naphtha and the tail gas of fractionation system II; 100% of the obtained wax oil is sent to the slurry preparation system for use as solvent oil. The oil residue slurry is sent to the oil residue slurry treatment system, and fluidized coking is used to obtain coke, tar and the tail gas of the oil residue slurry treatment system. The coking temperature is 500℃.

[0191] The yields of the main products are shown in Table 2.

[0192] Table 1. Composition of the slurries described in the examples and comparative examples, in kg.

[0193] slurry <![CDATA[Carbon-containing raw material 1 > <![CDATA[Solvent naphtha 2 > <![CDATA[Catalyst 3 > 1 100 (Coal A) 110 1 2 100 (waste tires) 120 0.1 3 100 (coal tar) 0 0.5 4 100 (Coal B + Waste Tires) 150 2 5 100 (Coal B + Coal A) 250 5

[0194] 1. Coal A is lignite; Coal B is bituminous coal; 2. The solvent oil in slurry 1 is a mixture of hydrogenated (15MPa, 360℃) products of a <520℃ distillate oil and wax oil mixture in a volume ratio of 1:1; the solvent oil in slurries 2 and 4 is the aforementioned <520℃ distillate oil and wax oil mixture in a volume ratio of 3:7; the solvent oil in slurry 3 is a 350-550℃ heavy oil hydrogenated distillate oil; the solvent oil in slurry 5 is a <520℃ distillate oil and wax oil mixture in a volume ratio of 7:3; 3. The catalyst contains... Based on the amount of active metal, the catalyst in slurry 1 is a FeOOH-based emulsifiable concentrate catalyst (with additives in wt%: 11% kaolin / 7% ZnO / 0.1% W / 0.5% Mo), the catalysts in slurries 2 and 3 are Fe2O3-based emulsifiable concentrate catalysts (with additives in wt%: 18% coke powder / 9% MnO2 / 5% ZnO), and the catalysts in slurries 4 and 5 are Fe2O3-based powder catalysts (with additives in wt%: 15% kaolin / 7% CaO / 0.1% Mo).

[0195] Table 2 shows the main products and coke yield (%) described in the embodiments, daf

[0196] Example 1 Example 2 Example 3 Example 4 Example 5 Comparative Example 1 naphtha 10.9 14.6 18.1 13.7 12.1 7.2 Aviation kerosene 22.5 15.8 21.9 18.3 15.7 18.3 diesel fuel 23.2 16.5 38.2 22.6 19.6 19.1 Wax oil - - 13.8 - 22.1 - Total oil yield 56.6 46.9 92.0 54.6 69.5 44.6

[0197] By comparing Example 1 and Comparative Example 1, it can be seen that Comparative Example 1 was conducted with the same slurry and conditions as Example 1, except that the feeding method of slurry 1 was not cyclone feeding. However, Comparative Example 1 had a significantly lower oil yield, with a total oil yield difference of up to 12% compared to Example 1.

Claims

1. A process for hydro-liquefaction and / or lightening of a carbonaceous feedstock, wherein, The method comprises: (1) mixing a carbon-containing raw material, solvent oil and a catalyst after pretreatment of the carbon-containing raw material to obtain a reaction slurry; the carbon-containing raw material is one or more selected from coal, biomass, industrial and domestic waste, inferior / heavy oil; (2) feeding the reaction slurry into a reactor of a slurry reaction system in a cyclone feeding mode to perform reaction to obtain a slurry reaction system light product and a slurry reaction system heavy product; (3) performing cyclone separation on the slurry reaction system light product to obtain a cyclone separation light product and a cyclone separation heavy product; (4) performing hot high-pressure separation on the cyclone separation light product to obtain a hot high-pressure separation oil and a hot high-pressure separation gas; (5) performing cold high-pressure separation on the hot high-pressure separation gas to obtain a cold high-pressure separation oil and a cold high-pressure separator tail gas; (6) performing gas-liquid separation on the slurry reaction system heavy product in a gas-liquid separation system I to obtain a gas-liquid separation system I light product and a gas-liquid separation system I heavy product; (7) performing condensate collection on the gas-liquid separation system I light product to obtain a condensate collection tank oil and a condensate collection tank tail gas; (8) mixing the hot high-pressure separation oil, the cold high-pressure separation oil and the condensate collection tank oil, and then performing purification treatment to obtain a purified crude oil and a crude oil purification system tail gas; (9) mixing the cyclone separation heavy product, the gas-liquid separation system I heavy product and the tar obtained in subsequent step (13), and then performing fractionation in a fractionation system I to obtain an oil residue slurry, a <520℃ distillate oil and a fractionation system I tail gas; mixing part or all of the <520℃ distillate oil with the purified crude oil to obtain an oil product upgrading reactor feed, and using the remaining part or all of the <520℃ distillate oil as the solvent oil; (10) performing upgrading treatment on the oil product upgrading reactor feed to obtain an oil product upgrading reactor product; (11) performing gas-liquid separation on the oil product upgrading reactor product in a gas-liquid separation system II to obtain a gas-liquid separation system II heavy product and a gas-liquid separation system II tail gas; (12) performing fractionation on the gas-liquid separation system II heavy product in a fractionation system II to obtain a wax oil, a diesel oil, a jet fuel, a naphtha and a fractionation system II tail gas; using part or all of the wax oil as the solvent oil, and discharging the remaining part or all of the wax oil as a product; (13) processing the oil residue slurry to obtain coke, tar and an oil residue slurry processing system tail gas; (14) combining, separating, enriching and purifying the cold high pressure separator off-gas, the condensate collection tank off-gas, the crude oil purification system off-gas, the fractionation system I off-gas, the gas-liquid separation system II off-gas, the fractionation system II off-gas and the oil sludge treatment system off-gas to obtain hydrogen, dry gas, liquefied petroleum gas (LPG), C5 + hydrocarbons and sulfur; the hydrogen is recycled after being combined with fresh hydrogen.

2. The method of claim 1, wherein, In step (1), the pretreatment is drying and grinding the carbon-containing raw material into a powder or slurry material.

3. The method of claim 1 or 2, wherein, The catalyst in step (1) is a suspended bed hydrogenation catalyst.

4. The method of claim 1 or 2, wherein, The solvent oil in step (1) is one or more of inferior oil / heavy oil and hydrogenation products thereof, coal tar and hydrogenation products thereof, coal tar distillate oil and hydrogenation products thereof, the <520℃ distillate oil obtained in step (9) and hydrogenation products thereof, or the wax oil obtained in step (12) and hydrogenation products thereof.

5. The method of claim 1 or 2, wherein, In step (1), the carbon-containing raw material, solvent oil and catalyst are mixed in a mass ratio of 100:(0-250):(0.1-5), and the amount of the catalyst is calculated based on active metals contained therein.

6. The method of claim 1 or 2, wherein, In step (2), the reaction is carried out at a temperature of 400-480℃, a hydrogen pressure of 2-10 MPa, and an average residence time of 15-120 min.

7. The method of claim 1 or 2, wherein, In step (3), the cyclone separation is carried out using a cyclone separation system.

8. The method of claim 1 or 2, wherein, In step (4), the hot high-pressure separation is carried out at a temperature of 200-450℃ and a pressure of 2-10 MPa.

9. The method of claim 1 or 2, wherein, In step (5), the cold high-pressure separation is carried out at a temperature of 0-80℃ and a pressure of 2-10 MPa.

10. The method of claim 1 or 2, wherein, In step (6), the gas-liquid separation is carried out using a high-pressure gas-liquid separator + a low-pressure gas-liquid separator in series, or a hydrocyclone.

11. The method of claim 1 or 2, wherein, In step (8), the purification treatment is carried out using one or more of filtration, centrifugation, sedimentation, and fractional distillation.

12. The method of claim 1 or 2, wherein, In step (9), the fractional distillation is carried out using vacuum distillation, or a combination of atmospheric distillation and vacuum distillation.

13. The method of claim 1 or 2, wherein, In step (10), the upgrading treatment is carried out using an upgrading reactor.

14. The method of claim 13, wherein, The conditions of the upgrading treatment are: temperature 280-410℃, pressure 5-25MPa, hydrogen / oil volume ratio 800-3000, volume space velocity 0.2-2h -1 .

15. The method of claim 1 or 2, wherein, In step (11), the gas-liquid separation is carried out using a high-pressure gas-liquid separator + a low-pressure gas-liquid separator in series, or a hydrocyclone.

16. The method of claim 1 or 2, wherein, In step (12), the fractional distillation is carried out using atmospheric distillation, or a combination of atmospheric distillation and vacuum distillation.

17. The method of claim 1 or 2, wherein, In step (13), the oil residue slurry is treated using fluidized coking, delayed coking, and / or solvent extraction.

18. The method of claim 17, wherein, The fluidized coking is carried out at a temperature of 500-800℃.

19. The method of claim 17, wherein, The delayed coking is carried out at a temperature of 500-700℃.

20. The method of claim 1 or 2, wherein, In step (14), the separation and enrichment is carried out using pressure swing adsorption, membrane separation, or cryogenic separation; and the purification treatment is carried out using an alcohol amine absorption method, a liquid phase oxidation-reduction method, a copper washing method, a crystalline sulfur method, or a Claus sulfur recovery method.

21. An apparatus for carrying out the method of any one of claims 1-20, the apparatus being used for processing one or more of carbon-containing feedstocks selected from coal, biomass, industrial and domestic waste, and inferior / heavy oil, the apparatus comprising a slurry preparation system, a slurry reaction system, a product separation system, an oil product upgrading system, an oil residue slurry treatment system, and a tail gas treatment system connected in fluid communication, wherein, the slurry reaction system comprises a cyclone feeder, a reactor, and one or more cyclone separators, the reactor being a gas-liquid-solid three-phase suspended bed reactor, the reactor comprising a reactor shell, a center pipe, a gas distributor, a feedstock slurry inlet, a light product outlet, and a heavy product outlet, the feedstock slurry inlet being connected to the cyclone feeder in fluid communication; the cyclone separators being located inside or outside the reactor; The product separation system comprises a light product separation system and a heavy product separation system, the light product separation system comprises a cyclone separation system, a hot high-pressure separator, a cold high-pressure separator and a crude oil purification system, the heavy product separation system comprises a gas-liquid separation system I, a condensate collection tank and a fractionation system I; wherein the cyclone separation system is connected to the light product outlet of the reactor or the outlet of the cyclone separator in a fluid communication manner, and the gas-liquid separation system I is connected to the heavy product outlet of the reactor in a fluid communication manner; The oil upgrading system comprises an oil upgrading reactor, a gas-liquid separation system II and a fractionation system II; The reactor shell comprises a cylindrical barrel, a bottom end hemispherical head and a top end hemispherical head; The gas distributor is arranged at the bottom end of the reactor, and the gas distributor comprises a gas inlet, a gas pre-distributor, a gas pre-distribution area, a partition plate, a transition pipe and a gas distribution ring pipe; A center pipe is arranged in the center of the cylindrical barrel, one end of the center pipe is fixed on the partition plate, and the other end of the center pipe is not connected with the top end hemispherical head; A conical plate is arranged below the liquid phase discharge port of the cyclone separator; Side lower gas injection holes are arranged on the gas distribution ring pipe; The slurry feeding pipe connected with the raw material slurry inlet forms an angle of 10-60 degrees with the wall of the reactor.

22. The apparatus of claim 21, wherein, The partition plate is arranged between the cylindrical barrel and the bottom end hemispherical head.

23. The apparatus of claim 21 or 22, wherein, The cyclone separator in the slurry reaction system is arranged at the top of the reactor or in a second cylindrical barrel arranged outside the reactor and in fluid communication with the reactor.

24. The apparatus of claim 21 or 22, wherein, The space between the bottom end hemispherical head of the reactor and the partition plate is a gas pre-distribution area, and the gas distribution ring pipe is arranged on the upper plane of the partition plate.

25. The apparatus of claim 24, wherein, Part of the gas distribution ring pipe is located in the center pipe, and the remaining part of the gas distribution ring pipe is located in the annular area formed by the center pipe and the cylindrical barrel.

26. The apparatus of claim 24, wherein, The transition pipe is vertically inserted into and fixed on the partition plate, and is in fluid communication with the gas pre-distribution area and the gas distribution ring pipe.

27. The apparatus of claim 21 or 22, wherein, Each component in contact with the partition plate is tightly fitted.

28. The apparatus of claim 21 or 22, wherein, The gas pre-distributor is located at the bottom end of the reactor.

29. The apparatus of claim 21 or 22, wherein, The raw material slurry inlet is arranged at the lower part of the cylindrical barrel of the reactor.

30. The apparatus of claim 21 or 22, wherein, The heavy product outlet is arranged at the bottom of the reactor.

31. The apparatus of claim 30, wherein, One end of the discharge pipe connected with the heavy product outlet is in communication with the center pipe.

32. The apparatus of claim 31, wherein, The discharge pipe passes through the partition plate and the bottom end hemispherical head of the reactor.

33. The apparatus of claim 21 or 22, wherein, The light product outlet is located at the top end of the reactor.

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